WO2021121453A1 - Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles - Google Patents

Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles Download PDF

Info

Publication number
WO2021121453A1
WO2021121453A1 PCT/DE2020/000306 DE2020000306W WO2021121453A1 WO 2021121453 A1 WO2021121453 A1 WO 2021121453A1 DE 2020000306 W DE2020000306 W DE 2020000306W WO 2021121453 A1 WO2021121453 A1 WO 2021121453A1
Authority
WO
WIPO (PCT)
Prior art keywords
flow
gas
pressure
adsorbent
heat exchanger
Prior art date
Application number
PCT/DE2020/000306
Other languages
German (de)
English (en)
Inventor
Andreas Hartbrich
Alexander Jekow
Ruprecht Marxer
Original Assignee
Silica Verfahrenstechnik Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Silica Verfahrenstechnik Gmbh filed Critical Silica Verfahrenstechnik Gmbh
Publication of WO2021121453A1 publication Critical patent/WO2021121453A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0438—Cooling or heating systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81—Solid phase processes
    • B01D53/82—Solid phase processes with stationary reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/249—Plate-type reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D21/0015—Heat and mass exchangers, e.g. with permeable walls
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0025—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being formed by zig-zag bend plates
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0031—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by paired plates touching each other
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
    • F28D9/0075—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements the plates having openings therein for circulation of the heat-exchange medium from one conduit to another
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
    • F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
    • F28F3/04—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element
    • F28F3/048—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element in the form of ribs integral with the element or local variations in thickness of the element, e.g. grooves, microchannels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2459—Corrugated plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2481—Catalysts in granular from between plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/3221—Corrugated sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32248—Sheets comprising areas that are raised or sunken from the plane of the sheet
    • B01J2219/32251—Dimples, bossages, protrusions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32279—Tubes or cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material
    • B01J2219/32475—Composition or microstructure of the elements comprising catalytically active material involving heat exchange

Definitions

  • the invention relates to a method for treating a raw gas loaded with at least one gaseous pollutant and / or useful component, in which the raw gas pressurized by a fan and / or compressor via an inflow-side distribution chamber at least one
  • Plate heat exchanger a multitude of flow channels filled with adsorbent, which are formed by corrugated and / or profiled sheets lying mirror-inverted, connected by webs and combined to form pairs of corrugated sheets, in parallel divided partial flows under adsorption pressure until the adsorbent is adsorbed with the pollutant.
  • the invention further relates to a device for carrying out the method, with at least one plate heat exchanger which comprises a plurality of flow channels and flow spaces perpendicular to these, which are formed by corrugated and / or profiled sheets of mirror-image superimposed, connected by webs, to form pairs of corrugated sheets are formed, wherein the flow spaces are arranged between the pairs of corrugated sheets, and the flow channels for the passage of the raw gas divided into partial flows are connected on the inflow side with a distribution space and on the outflow side with a collecting space, the upstream distribution space with a supply line for the raw gas and the downstream collecting space is in communication with a clean gas line, and the flow spaces open into a distribution space for the supply and discharge of a cooling or heating medium for indirect cooling or heating of the adsorbent, and with a he control unit that switches the plate heat exchanger loaded with the harmful and / or useful component from the adsorption to the regeneration state or vice versa to another plate heat exchanger.
  • Mainly adsorbents are used in the form of beds made of activated carbon, silica gel, aluminum oxide gel or molecular sieves, for example in a bed through which the gas to be cleaned flows (DE 35 05 351 A1, DE 197 54 185 C1, DE 198 09 200 A1 ), a bed arrangement of the adsorbent between heat exchanger plates (DE 103 61 515 A1, EP 2 718 086 B1, EP 1 284813 B1, DE 603 17 545 A2).
  • the gas to be cleaned flows through the adsorber filled with adsorbent, the adsorbent adsorbing the pollutant and heat is generated by the adsorption, which cannot be dissipated in conventional adsorbers.
  • the gas to be cleaned is therefore cooled before it enters the adsorber.
  • a temperature profile is created in the adsorber, ie at In the downward direction of flow of the gas through the adsorbent bed, the upper layers of the bed are cooled by the incoming gas and the lower layers are heated by the heat of adsorption released.
  • a substance adsorbs worse at a higher temperature and the maximum possible loading of the adsorbent with the adsorbed harmful component decreases with increasing temperature. This significantly limits the performance of the fixed bed adsorber.
  • the temperature profile that develops from VOC-contaminated exhaust air during the adsorption of solvents also favors the formation of fire-endangering hotspots in the activated carbon bed, which can lead to spontaneous combustion of the activated carbon.
  • a previously heated regeneration gas is introduced into the loaded adsorbent, which heats the adsorbent to a temperature at which the pollutant or the useful component desorbs.
  • Regeneration with gas is disadvantageous from an energetic point of view due to the relatively low heat capacity of the gas. All apparatus, pipes and fittings are heated up by the heated regeneration gas before the heat can heat up the adsorbent accordingly. This causes high operating costs due to the energy loss that has to be expended.
  • adsorbents such as activated carbon and silica gel are unsuitable for adsorption under high pressure, because at low partial pressure the adsorption capacity of activated carbon and silica gel is too low to be able to be used economically.
  • This prior art also suggests the desorption of the adsorbed Impurities from the adsorbent arranged in the fixed bed by stripping with a flushing gas, displacing with a preferably adsorbed material, heating the adsorbent to a temperature above the adsorption temperature in a direct or indirect way or releasing it to a pressure below the adsorption pressure.
  • the activated carbon When solvent recovery is used, the activated carbon is usually regenerated by direct steaming of the activated carbon with hot water vapor, which in addition to the heat losses also results in the solvent being contaminated by the steam. Furthermore, before the solvent can be reused, the water phase must be removed from the solvent, which in turn causes high expenditure in terms of energy and equipment.
  • the filling of tubes in a tube bundle with a circular ring cross-section (DE 37 29 517 A1) is known, concentric to the tube bundle a cooling leading cylindrical pipe coil and an electrical heating device is arranged in the center of the tube bundle and / or pipe run.
  • an apparatus in particular for use as a chemical reactor and / or adsorber and / or regenerator is known, which is constructed essentially cylindrically symmetrical about a preferred axis and contains at least two beds of particles that act catalytically and / or adsorptively and / or heat-storing.
  • the apparatus has means for supplying and removing gaseous or liquid media, which are each assigned to the ends of the beds facing away from one another and the ends facing one another.
  • a reactor comprising a heat exchange body defining one or more fluid flow channels and having a removable insert.
  • the insert includes a series of contact plates stacked along a common axis and press fit into one of the flow channels thereby providing secondary heat exchange surfaces in thermal contact with the primary wall surfaces.
  • the first possibility is to arrange the catalyst or adsorbent as a supported layer in the flow channel (EP 1 195 193 B1, EP 1 361 919 B1, EP 1 430 265 B1, DE 11 2006 000 447 T5, EP 1 434 652 B1, WO 03 / 095924 A1).
  • the particle size in these cases is less than 0.15 mm, so that this approach is suitable for flow channels with small cross-sections and closed flow channels of plate heat exchangers.
  • the catalyst or the adsorbent is introduced as a bed or packing into a relatively open, unimpeded flow passage with larger flow cross-sections (WO 2006/075 163 A2).
  • the particle sizes used here are more than 2 to 3 mm. If the catalyst packing is used up, it has to be removed from the flow channels by pressing the packing through a rod inserted into the flow channel.
  • the system is to a certain extent a one-way system, because the catalyst or the adsorbent can only be removed after it has been used up with a relatively high level of technical effort or the apparatus even has to be scrapped.
  • plate heat exchangers For small cross-sections of the flow channels, plate heat exchangers have therefore not been able to establish themselves as adsorption apparatus on an industrial scale.
  • the invention is based on the object of providing a method and a device with which it is possible, on an industrial scale, plate heat exchangers with slim flow channels for treating a raw gas loaded with at least one gaseous harmful and / or useful component by reducing the energy loss during adsorption and regeneration as well as reducing the risk of blockage of flow channels filled with adsorbents and the formation of fire-endangering hot spots, increasing the quality and speed of the regeneration process and making the raw gas pass the adsorbent while at the same time increasing profitability and security is largely avoided.
  • Substance exchange between a pollutant and / or useful component of a raw gas and the adsorbent to use small cross-sectional, slim flow channels of a cross-flow plate heat exchanger filled with adsorbent and at the same time to more effectively exchange heat with the adsorbent during adsorption and regeneration by dividing the raw gas and the flushing gas into partial flows design and to use the partial flows of the purge gas exclusively as a transport gas for the harmful and / or useful component.
  • Flow channels positioned flow chicanes and flow paths in the flow spaces for the flow guide and spacer plates forming the cooling or heating medium are achieved in the following steps: a) Simultaneous generation of turbulence in the partial flows of the raw gas within the flow channels and in the cooling medium within the flow spaces during adsorption or the partial flows of the purge gas in the
  • Flow channels and in the heating medium in the flow spaces during regeneration b) regulating the adsorption pressure in the flow channels during adsorption by throttling the outflow of clean gas from the collecting chamber to an overpressure of 0.1 to 15.0 bar, c) regulating the desorption pressure in the flow channels during regeneration by throttling the flow of purging gas into the distribution chamber to an absolute pressure of 0.01 to 1.0 bar while maintaining a vacuum pump vacuum on the suction side and d) regulating an overpressure of condensation when separating the desorption heated desorbate in a heat exchanger / condenser by means of condensation in the harmful and / or useful component and a return gas to a Overpressure of 0.1 to 5.0 bar by throttling the outflow of return gas from the heat exchanger / condenser.
  • the turbulence in the raw gas and in the purge gas are generated according to a preferred embodiment of the method according to the invention by flow chicanes that are formed as expressions perpendicular and / or transverse to the flow direction in the wall of the flow channel at the same time with the corrugated bending or corrugated rolling of the corrugated sheets, wherein the expressions can be aligned inwards into the flow channel and / or outwards into the adjacent flow spaces.
  • the generated turbulence counteracts the margins along the wall of the flow channels and also has the advantage that the cooling or heating medium is swirled directly on the surface by the features directed outwards into the flow spaces and thus improves the heat exchange.
  • the turbulence in the cooling or heating medium is generated by flow guide or spacer plates positioned in the flow spaces between the pairs of corrugated sheets, the cooling medium during adsorption or the heating medium during regeneration in a cross flow to the flow channels can be performed single or multiple.
  • the cooling or heating medium In the event that the cooling or heating medium is to be routed in several ways, adjacent flow spaces are alternately connected to one another, as a result of which the cooling or heating medium is diverted from flow space to flow space.
  • the flow guide and spacer plates in the flow spaces between the rows of flow channels constantly deflect the cooling or heating medium flowing past the flow channels, so that the indirect heat exchange with the adsorbent is highly effective.
  • the flow guide and spacer plates ensure an exact distance between the corrugated sheet metal pairs lying above or below one another and enable a stable and compact design.
  • the adsorption pressure is regulated such that the pressure of the raw gas in the Distribution chamber and the pressure of the clean gas in the collecting chamber are measured by pressure sensors connected to the control unit, the control unit compares the measured values with a specified setpoint value for the adsorption pressure (PAD) stored in the control unit and, if there is a deviation, the fan and / or compressor and a collecting chamber controls downstream pressure regulating valve, which adjusts the outflow of clean gas from the collecting chamber in such a way that the adsorption pressure corresponds to the setpoint value for the adsorption pressure.
  • PAD a specified setpoint value for the adsorption pressure
  • This control mode makes it possible to precisely and reliably maintain the adsorption pressure in the flow channels.
  • the desorption pressure is regulated in such a way that the pressure of the purging gas in the distribution chamber and the pressure of the vacuum pump applied in the collecting chamber are measured by pressure sensors connected to the control unit compares the setpoint for the desorption pressure stored in the control unit and, in the event of a deviation, controls the vacuum pump downstream of the collecting chamber and a control valve upstream of the distribution space, which adjusts the flow of flushing gas into the distribution space in such a way that the desorption pressure corresponds to the setpoint for the desorption pressure.
  • the advantage is that the desorption pressure in the flow channels can be precisely maintained through the interaction of the vacuum pump and control valve.
  • the condensation overpressure is regulated such that the pressure of the return gas is measured after leaving the heat exchanger / condenser by a pressure sensor connected to the control unit, the control unit the measured value with a predetermined, in the The control unit compares the setpoint for the condensation overpressure and, if there is a discrepancy, controls a pressure control valve downstream of the heat exchanger / condenser, which adjusts the return gas flow in such a way that the condensation overpressure corresponds to the setpoint for the condensation overpressure.
  • pure gas or inert gas is used as the flushing gas, which is divided into partial flows during the regeneration, each partial flow being passed into a flow channel filled with saturated adsorbent, flowing through this and the desorbed harmful and / or useful component discharges from the adsorbent into the collecting space and merged to desorbate from flushing gas and harmful and / or useful component.
  • a partial flow can be divided off from the clean gas generated by the method according to the invention and used as a flushing gas.
  • inert gas a corresponding reservoir is to be provided, from which the inert gas is supplied as a flushing gas.
  • the inert gas can also be taken from a supply network. Nitrogen is preferably used as the inert gas.
  • a particularly preferred embodiment of the method according to the invention provides that the partial flows of the raw gas during the adsorption and the partial flows of the purge gas during the regeneration are passed into flow channels filled with adsorbent and separated from one another in a gastight manner.
  • At least one groove is formed in the longitudinal direction of the webs for the insertion of a hard solder during corrugation rolling, which when the webs are superimposed in mirror image interlock and are firmly connected to one another by brazing, the webs in the transverse direction by laser welds be connected gas-tight.
  • the webs can, however, also be connected in a gas-tight manner in the longitudinal direction of the webs by at least one laser weld seam and in the transverse direction by a laser weld seam each sealing off with respect to the distribution space and the collecting space.
  • the partial flows of the raw gas during the adsorption and the partial flows of the purge gas during the regeneration are conducted into flow channels filled with adsorbent and which are in at least one flow connection with one another, the adjacent adjacent flow channels via at least one flow transition with passage openings for part of the partial flow entered in the flow channel of raw gas during adsorption and for part of the partial flow of flushing gas that has entered the flow channel communicate with one another during regeneration, through which at least two bypass flows are separated from the respective part of the partial flow and directed sideways into the adsorbent of the respective adjacent flow channel.
  • the flow transition is formed from a depression formed in the webs when the corrugated or profiled sheets are corrugated rolling, which is covered when the corrugated and profiled sheets are placed on top of each other by the area of the webs above and or below the webs lying on top of one another are materially connected by laser welding in the longitudinal and transverse directions, the laser weld seam being penetrated by the depression in the longitudinal direction and the depression being sealed gas-tight by weld seams in the transverse direction.
  • the flow transition can, however, also when the
  • Corrugated or profiled sheets are formed by a shallow gap between the webs, in that the webs are materially connected to one another in the longitudinal direction by laser line welding so that the gap interrupts the material connection and divides it into at least one flow transition section that passes through the web in the transverse direction of the webs Gap delimiting weld seams is sealed gas-tight.
  • several flow transitions in the longitudinal direction of the webs can be spaced apart and distributed uniformly or differently from one another.
  • the number of flow transitions in the webs in the vicinity of the The distribution space on the inflow side must be greater than the number of flow transitions in the webs near the collecting space on the outflow side, ie the number of flow transitions distributed along the webs can vary.
  • Another embodiment of the method according to the invention is characterized in that the condensed harmful and / or useful component is removed via a condensate drain and the return gas leaving the heat exchanger is mixed with the raw gas.
  • the further embodiment of the method according to the invention provides that beds of activated carbon granulate, aluminum oxide gel, silica gel, molecular sieves or mixtures thereof are used as the adsorbent.
  • Water or glycol-water mixtures can be used for cooling.
  • Steam, hot water or hot exhaust gases are used as the heating medium.
  • the plate heat exchanger is a modified cross-flow plate heat exchanger with slim flow channels which are spaced apart from one another by flow guide and spacer plates arranged in the flow spaces for the cooling or heating medium, the Flow channels have a clear width of at least 10 to a maximum of 120 mm and have flow chicanes inside to generate turbulence, and that the inflow-side distribution space with a flushing gas line for supplying the flushing gas and dividing it into partial flows and introducing them into the flow channels for the removal of the desorbed heated harmful and / or useful component from the adsorbent is connected as desorbate in the collecting chamber, the collecting chamber being assigned a pressure control valve for throttling the outflow of clean gas, and a control valve for throttling the purge gas line Inflow of flushing gas into the distribution space and the collecting space on the outflow side is connected to a vacuum pump on the suction side, and that the vacuum pump is connected on the pressure side to a heat exchanger
  • the device comprises the flow guide and spacer sheet a thin corrugated sheet with spacer profiles formed in the corrugation crests, exceeding the height of the corrugation crests, which are offset from one another from wave crest to wave crest with gaps, the spacer profiles in the corrugated sheet metal pairs formed by the webs of the corrugated sheet metal pairs lying above and below one another Engage in an offset supporting manner and the respective spacer profile is firmly fixed at the end on the associated pair of corrugated sheets.
  • the flow guide and spacer plates contribute to a compact design of the device according to the invention.
  • Partial flows in the flow channels past the adsorbent is that the flow chicanes are formed by shapes that are formed transversely and / or parallel to the flow direction of the partial flow of the raw gas or purging gas in the wall of the flow channels inwards and / or from the wall outwards.
  • the device is assigned a pressure sensor to measure the pressure of the raw gas, the pressure of the clean gas during adsorption and the pressure of the purge gas and the suction-side pressure of the vacuum pump during regeneration, the pressure sensors being associated with the distribution chamber and the collecting chamber connected to the control unit, which is connected to control the fan in the supply line, the pressure regulating valves to throttle the outflow of clean gas from the collecting chamber, the vacuum pump to generate a negative pressure during regeneration and the regulating valves to throttle the flow of purge gas into the distribution chamber .
  • the heat exchanger / condenser is connected on the downstream side to the supply line for the raw gas through the return gas line via the pressure control valve to throttle the outflow of return gas from the heat exchanger / condenser, a pressure sensor downstream of the heat exchanger / condenser for Measurement of the return gas pressure is provided, which is connected to the control unit which controls the pressure regulating valve so that the harmful and / or useful component can condense in the event of excess pressure.
  • the sieve can be dismantled from the flow channels and the used adsorbent can be easily removed via the distribution chamber on the supply side.
  • the filling of the flow channels with new adsorbent takes place after removing the downstream screen and reassembling the upstream screen vertically into the open flow channels via the downstream distribution space.
  • the modified cross-flow plate heat exchanger comprises a rectangular structural unit which is arranged in the interior of a rectangular or cylindrical housing, the distribution space being designed as a foot part, the collecting space being designed as a head part and the distribution space for the cooling or heating medium all Enclosing flow spaces open to flow.
  • This embodiment of the device according to the invention has the advantage that, depending on the prevailing operating conditions, the structural unit can be in a vertical or vertical position can be operated horizontally.
  • each structural unit is arranged one above the other in a common housing of the cross-flow plate heat exchanger and each structural unit is provided with an inflow-side distribution space and an outflow-side collecting space, the distribution spaces and the collecting spaces with one another through the flow channels with a clear width of 10 to 120 mm are flow-connected.
  • This arrangement enables free scaling of the gas quantities to be treated and simple assembly of the structural units.
  • the structural unit has an inflow-side floor and an outflow-side floor, the respective floor consisting either of a single molded part or of several molded parts adapted to the contour of the flow channels, which are firmly connected to each other and to the corrugated sheet metal bar .
  • a preferred embodiment of the device according to the invention is characterized in that the adjacent flow channels are separated from one another in a gas-tight manner.
  • the webs of mirror-inverted to each other arranged corrugated ⁇ or profile plates are connected together in longitudinal direction by at least one braze joint or at least one laser weld seam and in the transverse direction of the webs cohesively by means of laser welds, so that communication between adjacent flow channels is excluded.
  • the latter For the gas-tight connection of the webs, the latter have at least one groove running in the longitudinal direction of the webs for inserting a hard solder, the grooves interlocking when they are mirror-inverted and are connected to one another in a gastight manner by hard soldering.
  • the adjacent flow channels formed when the corrugated or profiled sheets are arranged in reverse order can be flow-connected by at least one flow transition running transversely to the longitudinal direction of the webs, the passage openings of which open into the adjacent flow channels at least one indentation (groove) formed in the web is formed, which is covered by the area above or below of the web, which is arranged laterally reversed, and that the webs lying on top of one another are gastight by at least one material connection (weld seam) penetrated by the recess and running in the longitudinal direction of the webs and the webs are connected in a gas-tight manner in the transverse direction by weld seams running parallel to the depression.
  • weld seam weld seam
  • the flow transition can, however, also consist of at least one shallow gap with passage openings between the webs which are materially bonded and gas-tight in the longitudinal direction, the webs being connected in a gas-tight manner in the transverse direction by a weld seam running parallel to the gap.
  • the passage opening of the flow transitions has a dimension which is smaller than the dimension and shape of the smallest particle size of the adsorbent bed, so that a passage of adsorbent from one flow channel into the adjacent other flow channel is excluded.
  • the flow transitions can be spaced apart from one another uniformly or at different lengths and distributed in the longitudinal direction of the webs.
  • This arrangement has the advantage that the partial flows of the raw gas flow separated by the passage openings can be distributed over the entire length of the flow channel in the adsorbent bed and help counteract incipient blockages in the narrow flow channels.
  • the flushing gas is air, preferably pure gas, or an inert gas, for example nitrogen.
  • the flushing gas preferably pure gas, or an inert gas, for example nitrogen.
  • a separate storage device or a corresponding supply network is provided, which is connected to the flushing gas line.
  • the adsorbent is a bed of activated carbon, aluminum oxide gel, silica gel, molecular sieves or mixtures thereof with a particle size between 0.6 mm and 6.0 mm.
  • the cross-flow plate heat exchangers consist of thin
  • Stainless steel, copper or aluminum sheet which is formed into corrugated or profiled sheet with different profile shapes by corrugating rollers.
  • the adsorbent-filled flow channels of the two cross-flow plate heat exchangers are arranged in a switchable manner via connecting lines and switching valves and the indirect cooling or heating for the adsorbent assigned to the flow spaces via the peripheral distribution space through connecting lines and shut-off valves via the control unit.
  • the heat generated during adsorption is removed from its place of origin by water or glycol / water mixtures, and the heat required to regenerate the adsorbent can be supplied where it is needed by steam, hot water or hot exhaust gases.
  • the adsorbent bed is heated on one side by the regeneration fluid, directed upwards or downwards.
  • the heat or desorption front migrates through the bed.
  • a large part of the components already desorbed in the hot area is adsorbed again in the not yet heated (cold) area of the adsorbent column and then has to be desorbed again in an energy-intensive manner.
  • the advantage of the solution according to the invention is, among other things, that the adsorbent located in the flow channels is heated at the same time. As a result, there are no cold areas in the bed of adsorbent in which desorbed components could be adsorbed again. This has the advantage that the energy efficiency of the process and the quality of the regeneration are significantly improved.
  • the flushing gas flow can be freely selected and only serves to remove the desorbed harmful and / or useful components, whereby higher concentrations of harmful and / or useful components can be set in the flushing gas and in particular the condensation quantities of harmful and / or useful components
  • Useful components such as dichloromethane, acetone, ethyl acetate, methanol, toluene, xylene, hexane, water reach orders of magnitude that meet industrial standards and are economical.
  • the lowering of the pressure during desorption also enables the amount of flushing gas to be minimized. For example, when the pressure is reduced to 0.5 bara and the flow rate in the adsorber remains the same, only half the amount of flushing gas is required. In addition, when the pressure is reduced, the required desorption temperature drops, which is particularly advantageous when recovering temperature-sensitive harmful and / or useful components such as chlorinated compounds.
  • the solution according to the invention thus opens up the possibility of using energy carriers such as hot water or even warm exhaust gas as a heating medium for the regeneration.
  • energy carriers such as hot water or even warm exhaust gas as a heating medium for the regeneration.
  • the condensation of the harmful and / or useful components is significantly more efficient, since the condensation is pressure-dependent.
  • a mixture of saturated air / ethyl acetate, for example, at a pressure of 1 barg and normal cold water (+ 2 ° C) achieves a condensation performance comparable to that at -10 ° C under normal pressure of 1 bara. Both the pressure and the temperature during the condensation can easily be adapted to the respective conditions.
  • a further advantage of the solution according to the invention is that the flushing gas does not have to transport the required desorption energy into the loaded adsorbent, but only transports the desorbed harmful and / or useful component away into the heat exchanger.
  • FIG. 1 a is a perspective exploded view of two pairs of corrugated iron, offset from one another and arranged in a mirror-inverted manner, with their webs lie on top of one another and are materially connected to one another by laser welding without a flow transition,
  • FIG. 1b shows a detail in plan view of FIG.
  • FIG. 1c shows a perspective illustration of the flow guide and spacer plate inserted in the flow spaces between the corrugated sheet metal pairs
  • FIG. 2a a perspective illustration of one of several
  • FIG. 3 is a side view of a modified cross-flow
  • FIG. 5a shows a side view of a modified cross-flow plate heat exchanger in the interior of a cylindrical housing
  • 5b is a side view of a modified cross-flow
  • Plate heat exchanger from, for example, two structural units arranged one above the other,
  • FIG. 6 shows a perspective exploded view of two mutually offset, mirror-inverted pairs of corrugated iron, the webs of which lie on top of one another and are provided with grooves in the longitudinal direction, which are connected to one another by brazing without a flow transition, Fig. 6a a through a web along the line A ⁇ A of Fig. 6,
  • Fig. 6b shows a section along the line B-B of Fig. 6a
  • Fig. 7b shows a section along the line D-D of Fig. 7a
  • Fig. 9a shows a section along the line F-F of Fig. 8,
  • Fig. 10 is a schematic representation of the inventive
  • FIG. 11 shows a schematic representation of the device according to the invention during the regeneration phase with simultaneous heating of the loaded adsorbent in the flow channels.
  • La shows the basic structure of pairs of corrugated sheets 7c, which consist of mirror-inverted corrugated sheets 7a and 7b made of stainless steel with a thickness of 0.3 mm. a modified cross-flow plate heat exchanger la or lb without flow transition.
  • the two corrugated sheets 7a and 7b which are made of stainless steel sheet, are placed one above the other in a mirror-inverted manner and, with their corrugated profiles 8, form vertical flow channels 9 that are parallel to one another and whose webs 10a and 10b face each other and by laser line welding in longitudinal direction LR along the edge of flow channels 9 and in transverse direction QR the webs 10a and 10b are welded gas-tight.
  • the flow channels 9 have, for example, a length L of up to 2 m and a clear width W of approximately 6 mm to 120 mm.
  • Adjacent pairs of corrugated sheets 7c of the corrugated sheets 7a and 7b arranged one above the other form flow spaces 14 through which a cooling or heating medium K or H can be passed in a cross-flow to the flow channels 9, i.e. simultaneously through the flow spaces 14.
  • Corrugated sheet metal pairs 7c formed in 7b are -as also shown in FIG.
  • spacer profiles 12 are formed at regular intervals from one another, each of which engages alternately in a supporting manner in the area of the corrugated sheet pairs arranged one above the other, the spacer profile 12 on the respective corrugated sheet pair 7c at the beginning and end with a material fit is attached, so that a displacement of the flow guide spacer plate 11 is excluded.
  • Wave crests WB of the flow guide and spacer plate 11 are arranged offset to one another on a gap 17, so that flow paths SF arise which force the cross-flow cooling or heating medium K or H to deflect and thereby generate turbulence.
  • An example of a flow path SF is indicated by arrows in FIG. Figures 2a and 2b illustrate the structure of one of several
  • Corrugated sheet pairs 7c composite adsorber unit 1.
  • the corrugated sheet pairs 7c penetrate with their open-ended flow channels 9 a head-side floor 18 and a downstream floor 19.
  • the floors 18 and 19 are composed of molded parts 18.1 to 18.n and 19.1 to 19.n, respectively Contour is adapted to the shape and dimensions of the corrugated sheet metal pairs 7c, expediently by laser cutting.
  • the molded parts are joined together with the inserted corrugated sheet metal pairs 7c along the contour and materially connected by laser welding or brazing, so that a substantially rectangular apparatus is created, which can be inserted either into a rectangular or cylindrical housing 2.
  • the joining direction is indicated by an arrow in FIG. 2b.
  • Plate heat exchangers la and lb are each housed as a structural unit in a housing 2 made of stainless steel.
  • the housing 2 consists of a rectangular housing shell 2a, in the interior of which the adsorber unit 1 is arranged.
  • the head-side bottom 18, together with a head part 20 belonging to the housing 2 is flanged at the end of the wall 13 of the housing shell 2a, so that a distribution space 3a or 3b is created on the inflow side, into which the crude gas G, which is contaminated with a gaseous harmful and / or useful component enters via a feed line 4 connected to the head part 20.
  • the bottom 19 of the adsorber unit 1 on the foot side and a foot part 21 flanged on the end face of the wall 13 of the housing shell 2a forms a collecting space 5a or 5b for the clean gas RG leaving the flow channels 9 and under adsorption pressure PAD, which is connected to the foot part 21 connected discharge line 6 of a gas expansion turbine (not shown) with a power generator or via an expansion valve to a consumer or as exhaust air into the atmosphere.
  • a gas expansion turbine not shown
  • the inflow-side distribution space 3a or 3b is located at the head of the cross-flow plate heat exchanger la or lb, whereby the flow direction SRR of the raw gas G runs vertically downwards through the adsorber unit 1.
  • the raw gas G can also flow vertically upwards through the adsorber unit 1.
  • the flow channels 9 filled with an adsorbent AM are preferably aligned vertically and connect the distribution chamber 3a or 3b with the collecting chamber 5a or 5b, open to flow.
  • the flow channels 9 are covered at the end with a removable gas-permeable sieve 22.
  • the sieve 22 has a mesh size that is selected to be smaller than the smallest particle size of the adsorbent AM filled into the flow channels 21, so that the adsorbent does not get out of the flow channels.
  • the granular adsorbent AM for example activated carbon, forms an elongated column of adsorbent in each of the flow channels 9.
  • the flow channels 9 have, for example, a clear width W of 6 mm and the diameter of the particles of the adsorbent is, for example, 1 mm.
  • the flow channels 9 - as shown in FIG. 4 - have flow baffles 24 which are molded into the wall 25 of the flow channels 9 in the form of impressions 26 when the corrugated sheets are manufactured.
  • the embossments 26 can extend from the wall 25 into the interior of the flow channel 9 and / or protrude from the wall 25 into the flow space 14.
  • a combination of inwardly projecting into the flow channel 9 and outwardly into the flow spaces 14 is also possible.
  • the expressions are designed as elongated bodies which are arranged transversely and parallel to the flow direction SRR of the partial flow TG of the raw gas G along the wall 25 of the flow channels.
  • the flow baffles 24 have the effect that the raw gas G or flushing gas SG located in the vicinity of the wall is directed into the interior of the flow channel 21, as a result of which turbulence is generated, which largely prevents access to the edge.
  • the adsorber unit 1 arranged in the interior of the housing 2 is surrounded by a distribution space 15 for the supply and discharge of a cooling medium K or a heating medium H, which is formed between the wall 13 of the housing shell 2a and the adsorber unit 1 is (see Fig. 3, 5a and 5b).
  • Adjacent pairs of corrugated sheet metal 7c form flow spaces 14 with one another, which open into the distribution space 15 so that the cooling medium K or the heating medium H can be guided through the flow spaces 14.
  • the flow guide and spacer plates 11 located in the flow spaces 14 ensure that turbulences arise in the cooling or heating medium K or H, which significantly improve the effectiveness of the heat exchange during adsorption and desorption.
  • Fig. 5a the cross-flow plate heat exchanger la or lb is shown, which receives an adsorber unit 1 in the interior of its cylindrical housing 2.
  • the head-side bottom 18 of the adsorber unit 1 is superimposed on the wall 13 of the housing shell 2a of the housing 2 and is together with the head part 20 in the form of a dished bottom and the foot-side bottom 19 of the adsorber unit 1 with the foot part 21 forehead or. flanged on the foot side to the wall 13 of the cylindrical housing jacket 2.
  • the distribution space 3a or 3b and the collection space 5a or 5b are formed by the head part 20 and the foot part 21 with the corresponding bottoms 18 and 19 of the adsorber assembly 1, respectively.
  • Fig. 5b for example, two adsorber units 1 arranged vertically one above the other are accommodated in the common housing 2, each unit 1 having an inflow-side distribution space 3a or 3b, an outflow-side collecting space 5a or 5b and a distribution space 15 for the cooling and Heating medium H or K is provided.
  • the distribution spaces 3a and 3b and the collecting spaces 5a and 5b are flow-connected to one another through the flow channels 9. This has the advantage that the gas quantities to be treated can be freely scaled.
  • the raw gas G is pressed by a fan 23 (see FIGS. 10 and 11), for example a rotary piston blower, at a pressure of 4.0 bar via the supply line 4 into the distribution chamber 3a or 3b.
  • the raw gas G is divided into individual substreams TG in the distribution chamber 3a or 3b, one substream each entering a flow channel 21 and flowing through the adsorbent bed AM in a vertically downward direction, the harmful and / or useful component being adsorbed on the adsorbent.
  • the partial flows TG leaving the flow channels 9 as pure gas RG collect in the collecting space 5a or 5b and are discharged via the discharge line 6.
  • the webs 10a and 10b can also be connected in a gas-tight manner in the longitudinal direction LR by a brazed connection 29c and in the transverse direction QR by laser welds 29b.
  • at least one groove R is formed in the webs 10a and 10b.
  • the grooves R each run in the longitudinal direction LR along the flow channels 9.
  • the grooves R have such a geometry and shape that before the corrugated or profiled sheets 7a or 7b are placed on top of one another in a mirror image, a hard solder is inserted into the Groove R of the web 10a of the lower corrugated or profiled sheet can be inserted.
  • the groove R of the web 10b located above comes to rest on the brazing alloy lying in the groove R of the web 10a below, and the interlocking grooves are connected in a gastight manner by the brazing material under the influence of temperature.
  • the webs 10a and 10b are sealed off from the distribution space 3a or 3b and the collecting space 5a or 5b by laser weld seams 29b.
  • 7, 7a, 7b and 7c show a second embodiment variant of the
  • At least one indentation 27a or 27b is formed in the web 10a or 10b transversely to the longitudinal direction LR over the entire width B when the corrugated or profiled sheets 7a and 7b are rolled, which when the two corrugated or profiled sheets 7a and b the parallel adjacent flow channels 9 connects to one another in an open-flow manner.
  • the depression 27a or 27b has a depth T which is smaller than the smallest particle size of the adsorbent, so that no adsorbent can get from one flow channel into the other flow channel (see FIG. 7a).
  • the depressions 27a and 27b are each laterally reversed and are covered by the web 10a and 10b of the corrugated or profiled sheet 7a and 7b located above and below.
  • the flat areas of the webs 10a and 10b facing one another are superimposed on one another and support one another.
  • the webs 10a and 10b are mechanically pressed together, fixed and welded to one another in a gas-tight manner by laser welding in the longitudinal direction LR.
  • the depressions 27a and 27b thus penetrate the weld seam 29a running in the longitudinal direction LR between the webs 10a and 10b in the transverse direction QR.
  • the gas-tight connection between the webs 10a and 10b lying one above the other in the transverse direction QR is made by further weld seams 29b running parallel to the depression 27a and 27b, as can be seen from FIGS. 7b and 7c.
  • the depressions 27a and 27b represent depressions in the webs 10a and 10b, the superimposed webs in the area of the depressions 27a and 27b do not touch and remain unwelded, so that a flow transition 30 is created with passage openings 31, which into the respectively adjacent Flow channels 9 open.
  • A penetrates through the flow transition 30 during adsorption
  • the cross-sectional area QF of the passage opening 31 depends on the geometry and shape of the depression 27a or 27b.
  • the dimensions of the passage opening 31 are selected so that the adsorbent with its smallest grain cannot pass through the passage opening.
  • Plate heat exchanger la or lb is shown in Fig. 8 in conjunction with Fig. 9a and 9b.
  • the flow transition 30 is through a shallow gap 28 when loose Superimposing the corrugated or profiled sheets formed between the webs 10a and 10b.
  • the webs 10a and 10b are connected to one another in a gas-tight manner by a weld seam 29a running in the longitudinal direction LR, which is interrupted by at least one gap 28.
  • the gap 28 represents a flow transition 30 with a passage opening 31, which connects the adjacent flow channels 9 to one another in an open-flow manner.
  • the gap 28 is sealed gas-tight in the transverse direction QR of the webs 10a and 10b by weld seams 29b (see FIG. 9b).
  • the size of the bypass flows BS reaching the flow channels 9 can be influenced by the number, geometry and shape of the flow transitions 30.
  • the number of flow transitions 30 between adjacent flow channels 9 can be increased or reduced so that the cross-sectional area QF of all passage openings 31 can be varied, a design of the flow transitions 30 depending on the type and nature of the adsorbent AM is possible and a blockage of the Flow channels 9 can be counteracted by a uniform or uneven distribution of the bypass flows BS over the adsorbent column.
  • FIG. 10 shows the cross-flow plate heat exchanger la during adsorption with simultaneous cooling and the cross-flow plate heat exchanger lb in the regeneration mode before switching to the adsorption mode.
  • Plate heat exchangers la and lb are each connected by a connecting line 32a and 32b, which can be opened or closed by a shut-off valve 33 assigned to the distribution space 3a and integrated into the connection line 32a and a shut-off valve 34 assigned to the distribution space 3b and integrated into the connection line 32b.
  • a connecting line 32a and 32b opens Feed line 4 into which a fan or a compressor 23 is integrated, which pressurizes the raw gas G and presses it into the corresponding distribution spaces 3a or 3b.
  • a pressure sensor 33 is arranged in the distribution chamber 3a or 3b, which measures the pressure PG of the raw gas G before the partial flows TG of the raw gas G enters the flow channels 9 and forwards the measured values to the control unit 37 via the control line 36.
  • a pressure sensor 38 is arranged in the collecting space 5a or 5b, which continuously measures the pressure PRG of the pure gas RG and transmits the measured values to the control unit 37.
  • the control unit 37 is based on an existing process design that takes into account the type, nature and quantity of the pollutant and / or useful component in the raw gas G, the limit values to be achieved for the pollutant concentrations in the clean gas RG and the operating data, setpoint values for the adsorption pressure PAD, the Desorption pressure PD and the condensation overpressure rk are stored.
  • the adjustment of the adsorption pressure PAD to an overpressure between 1.0 and 15.0 bar takes place in such a way that the control unit 37 compares the pressure values measured by the pressure sensors 33 or 38b with the setpoint value of the adsorption pressure PAD and, in the event of a deviation from the setpoint value, the fan and / or the compressor 23 and a pressure control valve 39 integrated in the connecting line 44a, which adjusts the adsorption pressure PAD to the specified target value by throttling the outflow of the clean gas RG from the collecting chamber 5a or 5b.
  • the flow of the raw gas G is indicated by a non-blackened arrow in the supply line 4 and the connecting line 32a.
  • the two supply lines 41a and 41b each bind in the direction of flow after the shut-off valve 33 or 34 in the connecting line 32a or 32b and can be opened or closed by a shut-off valve 42 or 43, so that the Purge gas SG according to the operating state of the cross-flow plate heat exchanger la or lb can be switched on or off via the control unit 37.
  • Plate heat exchangers la and lb each lead a connecting line 44a and 44b into the discharge line 6 for the clean gas RG.
  • Shut-off valves 45 and 46 are integrated into the connecting lines 44a and 44b, which are connected to the control unit 37 via control lines 36 and can be opened or closed accordingly, the shut-off valve 45 being assigned to the collecting space 5a and the shut-off valve 46 being assigned to the collecting space 5b.
  • shut-off valves 33, 34, 42, 43, 45 and 46 are also connected to the control unit 37, which issues the commands for the respective opening or closing of the valves.
  • Plate heat exchangers 1 a or 1 b an inflow-side connecting line 47 for a cooling medium K, for example water, opens into the peripheral distribution space 15, in which the flow spaces 14 are arranged so as to be open to flow.
  • a cooling medium K for example water
  • the cooling medium K enters all flow spaces 14 at the same time, is set in turbulence by the flow guide and spacer plates 11 between the corrugated sheet metal pairs 7c, flows around the flow channels 9 and absorbs the heat of adsorption by indirect heat exchange.
  • the heated cooling medium K is discharged via a discharge line 49a that can be opened or closed by a shut-off valve 48a.
  • the direction of flow of the cooling medium is indicated by arrows.
  • a connecting line 52 is provided, which can be opened or closed by shut-off valves 50 and 51, which is connected to a feed line 54.
  • the direction of flow of the heating medium H is indicated by arrows (see also FIG. 11).
  • the connecting line 47 stands for the two distribution spaces 3a and 3b with a supply line 53 for supplying the cooling medium K, for example water at a temperature of 25 ° C, into the flow spaces 14, the connecting line 47 being opened by a shut-off valve 55 or 56, which is electrically connected to the control unit 37 via the control line 36 or can be closed.
  • the flow spaces 14, which are in flow connection with the connecting line 47 are connected to a discharge line 59a, which can be opened and closed by shut-off valves 57a and 58a, for discharging the condensate H and emptying the cooling medium K from the flow spaces 14.
  • the flow spaces 14 of the cross-flow heat exchanger 1b are also connected to a discharge line 59b for the condensate H and the cooling medium K.
  • a shut-off valve 60a for the condensate H and a shut-off valve 60b for the cooling medium K are correspondingly integrated into the discharge line 59b.
  • the connecting lines 44a and 44b are mutually through a
  • Meshed desorbate line 61 which in the flow direction of the clean gas RG integrates into the respective connecting line 44a and 44b upstream of the shut-off valves 45 and 46, the desorbate line 61 being opened or closed by a shut-off valve 62 opposite the connecting line 44a and a shut-off valve 63 opposite the connecting line 44b can.
  • the shut-off valves 62 and 63 receive the actuating commands required for this from the control unit 37.
  • a discharge line 64 branches off between the shut-off valves 62 and 63, which is connected to a vacuum pump 65, which in the collecting space 5a or 5b and the flow channels 9, depending on the harmful and / or useful component, has an absolute pressure of 0.9 generated bar, so that the desorbed harmful and / or useful component is transported away from the collecting space 5a or 5b in the suction flow with the flushing gas SG.
  • the direction of flow of the desorbate DS is indicated by an arrow with a point (see also FIG. 11).
  • the pressure side of the vacuum pump 65 is with one through one with
  • Water-cooled heat exchanger / condenser 66 connected, in which the sucked harmful and / or useful component in the desorbate DS condenses by cooling and the condensate via a with the heat exchanger / condenser 66 connected condensate drain 67 is discharged.
  • the gas leaving the heat exchanger / condenser 66 is fed as return gas GR with a residual charge above the respective VOC limit value via a return gas line 68 in the direction of flow upstream of the fan 23 into the supply line 4 of the cross-flow plate heat exchanger la or lb, which is in adsorption
  • the pressure control valve 69 integrated into the return gas line 69 throttles the pressure of the return gas GR so that the condensation of the harmful and / or useful components in the heat exchanger / condenser 66 can take place at an overpressure of 0.1 to 5.0 bar.
  • the direction of flow of the return gas GR is indicated by arrows (see FIGS. 10 and 11).
  • the shut-off valve 33 is open and the shut-off valve 34 assigned to the distribution space 3b is closed.
  • the shut-off valve 45 assigned to the collecting space 5a in the connecting line 44a is open and the shut-off valve 46 belonging to the collecting space 5b is closed.
  • shut-off valve 55 in the connecting line 47 and the shut-off valve 48a in the discharge line 49a belonging to the cooling K of the cross-flow plate heat exchanger la connected to adsorption are open, whereas the shut-off valve 56 in the connecting line 47 to the cross-flow plate heat exchanger lb, the shut-off valves 60b and 60a in the discharge line 59b from the cross-flow plate heat exchanger lb, the shut-off valve 50 belonging to the heater H in the connecting line 52 are closed.
  • the raw gas G thus reaches the distribution space 3a and is divided into partial flows TG which, for example, flow vertically upwards into the flow channels 9 filled with adsorbent AM.
  • the noxious and / or useful components in the raw gas G are adsorbed on the adsorbent AM and the concentration front that forms moves vertically upwards through the adsorbent column of the respective flow channel 9 until the concentration front breaks through, ie the noxious and / or useful component in the collecting space 5a or 5b is detectable in measurable quantities.
  • gas sensors 70 connected to the control unit 37 are provided to detect the breakthrough and are arranged in the distribution space 3a or 3b and in the collecting space 5a or 5b.
  • the gas sensors 70 determine the input concentration the harmful and / or useful component in the distribution chamber 3a or 3b and the output concentration in the collecting chamber 5a or 5b and transfer this information to the control unit 37, which evaluates the data and the corresponding control commands to close the shut-off valve 33 in the connecting line 32a and open the shut-off valve 34 outputs in the connecting line 32b, so that the raw gas G is directed to the previously regenerated cross-flow plate heat exchanger 1b.
  • the cross-flow plate heat exchanger lb is in the desorption state. Before the desorption process begins, the cooling water in the flow spaces 14 of the cross-flow plate heat exchanger 1b is first emptied via the open shut-off valve 60a in the discharge line 59b,
  • the shut-off valve 34 is in the connection line 32b, the shut-off valve 62 in the desorbate line 61, the shut-off valve 46 in the connection line 44b, the shut-off valve 56 in the inflow-side connection line 47 for the cooling medium K, the shut-off valve 60a in the discharge line 59b for the cooling medium K and the condensate H and the shut-off valve 48b in the discharge line 49b on the outflow side are closed, while the control valve 43 in the supply line 41b for the flushing gas SG, the shut-off valve 51 in the connecting line 52 for the heating medium H, the shut-off valve 60b, the shut-off valve 63 in of the connecting line 44b and the pressure control valve 69 in the return gas line 68 are open.
  • a partial flow of the clean gas RG arrives as flushing gas SG via the flushing gas line 40 and the supply line 41b in the distribution space 3b and splits into partial flows TS which enter the open flow channels 9, where the flushing gas SG comes into contact with the loaded adsorbent AM comes.
  • the direction of flow of the purge gas SG is indicated by black dots in FIG. 11.
  • the heating medium H here water vapor
  • the peripheral distribution space 15 When the shut-off valve 51 is open at the same time, the heating medium H, here water vapor, flows through the peripheral distribution space 15 and enters the flow spaces 14, which open into the peripheral distribution space 13, so that the heating medium H absorbs the saturated adsorbents AM and AM in the flow channels 9 the upward flowing purge gas SG flows around and indirectly heats up.
  • the adsorbent located in flow channels and saturated with the harmful and / or useful component is heated until the harmful and / or useful component is desorbed.
  • the desorption temperature depends on the regulated absolute pressure and the material properties of the harmful and / or useful component to be removed.
  • the pressure sensors 35 and 38 arranged in the distribution chamber 3a and 3b and in the collecting chamber 5a and 5b, the pressure psG of the inflowing purge gas SG and the pressure PDS of the outflowing desorbate DS are measured, which is caused by the negative pressure pv of the vacuum pump 65 in the suction flow from the Collection space 5a or 5b is transported away.
  • the pressure sensors 35 and 38 transmit the measured values of the pressure to the control unit 37.
  • the adjustment of the desorption pressure PD to an absolute pressure of 0.01 to 1.0 bar takes place in such a way that the control unit 37 compares the pressure values transmitted by the pressure sensors 33 and / or 38 with a predetermined setpoint value of the desorption pressure PD stored in the control unit 37 and in case of deviation from the desired value, the vacuum pump 65 and a the distribution chamber 3a or 3b upstream of control valve 42, 43 controls which adjusts the inflow of purge gas SG in the distribution chamber 3a and 3b that the desorption D which stored in the control unit 37, target value corresponds to.
  • the desorbate DS collects in the collecting space 5b and is sucked in by the vacuum pump 65 and conveyed on the pressure side via the discharge line 64 into a heat exchanger / condenser 66, in which the harmful and / or useful component condenses by cooling and discharged via a condensate drain 67 for further use becomes.
  • the condensation of the harmful and / or useful component is carried out so that the return gas pressure PGR of the return gas GR after leaving the Heat exchanger / condenser 66 is measured with a pressure sensor 71 and the measured values are transmitted to the control unit 37.
  • the adjustment of the condensation overpressure rk to an overpressure of 0.1 to 5 bar in the heat exchanger / condenser 66 takes place in such a way that the control unit 37 compares the pressure value transmitted by the pressure sensor 71 with the specified target value of the condensation overpressure rk and if it deviates from the target value adjusts the pressure regulating valve 69 so that the condensation overpressure rk in the heat exchanger / condenser 66 corresponds to the setpoint stored in the control unit 37.
  • the control unit 37 connected to the gas sensor 70 issues control commands to the shut-off valve 51 and the Control valve 43 to close, so that on the one hand the heat exchange between the heating medium H and the adsorbent and on the other hand the supply of flushing gas SG is interrupted.
  • the shut-off valves 56 and 48b belonging to the cooling K open whereby the cooling medium enters the flow spaces 14 and the heated adsorbent AM located in the flow channels 9 is cooled to a temperature which is suitable for a renewed adsorption process.
  • the adsorbent is thus activated.
  • the cross-flow plate heat exchanger lb is ready for a new adsorption process.
  • Purge gas SG serves exclusively as a transport medium for the desorbed harmful and / or useful component and has no heating function for the adsorbent and, on the other hand, the desorption energy to be applied for desorption through an indirect heat exchange of the heating medium H with the adsorbent AM filled in the flow channel 9 at the place where it is needed, is applied.
  • Another advantage is that the desorption can be carried out at an absolute pressure, for example 0.9 bara, and the condensation can be carried out under excess pressure, for example 1.0 barg.
  • the negative pressure in the flow channels 9 is set by regulating the supply of purge gas SG via the control valves 42 and 43, which are connected to the control unit 37, which outputs the control commands to the control valves depending on the harmful or useful component in the raw gas RG.
  • a company processing the solvent acetone has one
  • Exhaust air cleaning system to remove solvents that are used, for example, in the coating of foils, and to clean the exhaust air accordingly.
  • free emissions can occur in the production hall, which are led to the exhaust air purification system with suction devices in order to guarantee compliance with the maximum workplace concentration in the hall.
  • This exhaust air arising from the hall and the exhaust air cleaning system is to be cleaned or treated with the method according to the invention.
  • Adsorbent activated carbon with a grain size of 1 to 4 mm. Length of the flow channels: 1,000 mm per unit of light. Width of the flow channels: 20 mm. Number of adsorber units: 5
  • Adsorption heat to be dissipated approx. 6.5 kW per adsorber unit, total approx. 32.5 kW
  • Cooling medium cooling water, 25 ° C
  • Cooling water requirement for adsorption approx. 1.2 m 3 / h per unit, total approx. 6.0 m 3 / h adsorption time: 30 minutes
  • Heating medium hot water, 90 ° C desorption pressure: ⁇ 100 mbar desorption temperature: approx. 85 ° C
  • the method according to the invention proceeds as follows.
  • the untreated exhaust air as raw gas G is fed into the distribution space 3a of the cross-flow plate heat exchanger la via the supply line 4 and the fan 23, which conveys the exhaust air at a pressure of 1.1 bar a into the distribution space 3a.
  • the modified cross-flow plate heat exchanger 1a comprises a
  • the vertical flow channels 9 are flowed around in a cross flow by a cooling or heating medium, which is set in turbulence by the flow guide and spacer plates 11, whereby the im Flow channel 9 taking place on the adsorbent AM is in heat exchange with the cooling medium K, so that the resulting adsorption heat is dissipated where it is generated, improves the absorption capacity of the adsorbent and counteracts the formation of fire-endangering hot spots.
  • 5 adsorber units 1 with the structure described above are accommodated in a common housing 2 of a cross-flow plate heat exchanger la or lb (see FIG. 5b).
  • Two of these cross-flow plate heat exchangers la form the adsorption device, with one cross-flow plate heat exchanger alternately in the adsorption phase and the other cross-flow plate heat exchanger in the regeneration phase.
  • Activated carbon with a grain size of 1 to 4 mm is used as the adsorbent, which is poured into the flow channels 9.
  • the flow transitions 30 existing between the flow channels 9 allow at least one bypass flow into the adjacent flow channels 9.
  • the flow chicanes 24 arranged in the flow channels 9 counteract the marginal accessibility in the flow channels 9 by generating turbulence.
  • the flow channels 9 are loaded for a total of 30 minutes and the regeneration of the activated carbon takes 20 minutes, followed by cooling the adsorbent for 10 minutes.
  • the energy required for cooling during the 30-minute adsorption is approx. 6.5 kW per unit and hour.
  • the 5 adsorber units 1 require a cooling capacity of approx. 16.5 kWh.
  • the discharged cleaned exhaust air contains less than 50 mg / m 3 acetone as a half-hourly mean value according to TA-Luft.
  • a desorption energy of approx. 10 kW is required per adsorber unit 1.
  • a heating output of approx. 17 kWh is required for the 5 adsorber units.
  • the relatively highly concentrated exhaust air can be fed directly to the cross-flow plate heat exchanger without dilution and without pre-cooling.
  • the risk of the formation of hot spots when removing highly concentrated ketones such as acetone with activated carbon is minimized due to the cooling.
  • the desorption of the solvent under vacuum reduces the desorption temperature and thus the necessary desorption energy, which is indirect is entered into the adsorbent, so that only a small flow of purging gas, preferably nitrogen, is necessary for discharging the solvent.
  • the downstream condensation under an overpressure of 5 bar enables the pure solvent to be separated off at a relatively high condensation temperature of 25 ° C.
  • concentrated exhaust air can also be processed in a similar form with other solvents, for example gasoline, toluene, dichloromethane, ethanol, to name just a few common pollutants.
  • solvents for example gasoline, toluene, dichloromethane, ethanol, to name just a few common pollutants.
  • the residual concentrations achieved with the method according to the invention correspond to the current legal requirements, for example at 20 mg / m 3 or 50 mg / m 3 .
  • the heat generated during adsorption can be continuously removed from its place of origin by water or glycol / water mixtures and thus counteract the formation of fire-endangering hot spots.
  • the heat required to regenerate the adsorbent is supplied by steam, hot water or hot exhaust gases and is available where it is needed to regenerate the adsorbent;
  • the adsorbent bed is heated upwards or downwards by the regeneration fluid on one side.
  • the heat or desorption front migrates through the bed.
  • Some of the components already desorbed in the hot area are adsorbed again in the not yet heated (cold) area of the adsorbent column and then have to be desorbed again in an energy-intensive manner;
  • the flushing gas flow can be freely selected and only serves to remove the desorbed harmful and / or useful components, which means that higher concentrations of harmful and / or useful components can be set in the flushing gas and, in particular, the condensation quantities of harmful and / or useful components such as dichloromethane , Acetone, ethyl acetate, methanol, toluene, xylene, hexane, water reach dimensions that meet industrial standards and are economical;
  • the lowering of the pressure during desorption enables the amount of flushing gas to be minimized.
  • the required desorption temperature drops, which is particularly advantageous when recovering temperature-sensitive harmful and / or useful components such as chlorinated compounds.
  • lowering the pressure can significantly increase the quality and speed of the regeneration process;
  • the solution according to the invention opens up the possibility of using energy sources such as hot water or even warm exhaust gas as a heating medium for regeneration;
  • Adsorber assembly 1 cross-flow plate heat exchanger la, lb housing from la, lb 2 Housing jacket 2a inflow-side distribution space of la, lb 3a, 3b

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un procédé et un dispositif pour traiter un gaz brut chargé en composants nuisibles et/ou utiles à l'échelle industrielle. À cet effet, l'on utilise au moins un échangeur de chaleur (1a, 1b) à plaques à courants inversés modifié comportant des canaux d'écoulement (9) ouverts aux passages de gaz, de la chambre de distribution (3a, 3b) à la chambre de collecte (5a, 5b), et présentant un diamètre intérieur (W) compris entre au minimum 10 et au maximum 120 mm, des chicanes d'écoulement (24) dans les canaux d'écoulement (9) et des trajets d'écoulement (SF) se trouvant dans les chambres d'écoulement (14) pour les tôles de guidage d'écoulement et d'espacement (11) formant le moyen de refroidissement ou de chauffage. Les chicanes d'écoulement et les trajets d'écoulement produisent des turbulences dans les écoulements respectifs. Une surpression ou une dépression et la température lors de l'adsorption ou de la désorption sont régulées par des soupapes disposées de façon correspondante et une pompe à vide, et le désorbat est condensé et ainsi récupéré.
PCT/DE2020/000306 2019-12-17 2020-12-04 Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles WO2021121453A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE102019008705 2019-12-17
DE102019008705.4 2019-12-17
DE102020007213.5 2020-11-25
DE102020007213.5A DE102020007213A1 (de) 2019-12-17 2020-11-25 Verfahren und Vorrichtung zum Behandeln eines mit Schad- und/oder Nutzkomponenten belasteten Gases

Publications (1)

Publication Number Publication Date
WO2021121453A1 true WO2021121453A1 (fr) 2021-06-24

Family

ID=76085297

Family Applications (4)

Application Number Title Priority Date Filing Date
PCT/DE2020/000304 WO2021121451A1 (fr) 2019-12-17 2020-12-04 Procédé et réacteur pour réactions catalytiques exothermes en phase gazeuse
PCT/DE2020/000305 WO2021121452A1 (fr) 2019-12-17 2020-12-04 Procédé et adsorbeur à profilé creux destiné au traitement d'un gaz chargé de composants nocifs et/ utiles
PCT/DE2020/000303 WO2021121450A1 (fr) 2019-12-17 2020-12-04 Appareil de froid à adsorption et procédé pour produire du froid d'adsorption à partir de chaleur
PCT/DE2020/000306 WO2021121453A1 (fr) 2019-12-17 2020-12-04 Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles

Family Applications Before (3)

Application Number Title Priority Date Filing Date
PCT/DE2020/000304 WO2021121451A1 (fr) 2019-12-17 2020-12-04 Procédé et réacteur pour réactions catalytiques exothermes en phase gazeuse
PCT/DE2020/000305 WO2021121452A1 (fr) 2019-12-17 2020-12-04 Procédé et adsorbeur à profilé creux destiné au traitement d'un gaz chargé de composants nocifs et/ utiles
PCT/DE2020/000303 WO2021121450A1 (fr) 2019-12-17 2020-12-04 Appareil de froid à adsorption et procédé pour produire du froid d'adsorption à partir de chaleur

Country Status (2)

Country Link
DE (4) DE102020007211A1 (fr)
WO (4) WO2021121451A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114042363A (zh) * 2021-10-28 2022-02-15 西安建筑科技大学 一种抑制脱硫脱硝活性炭自燃的吸附塔及方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102022000430A1 (de) 2022-01-26 2023-07-27 Apodis Gmbh Brennstoffzellensystem für ein Brennstoffzellenfahrzeug
DE102022000431A1 (de) 2022-01-26 2023-07-27 Apodis Gmbh Brennstoffzellensystem für ein Brennstoffzellenfahrzeug

Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1272891B (de) 1960-09-16 1968-07-18 Union Carbide Corp Verfahren zum Reinigen von Gasen oder Daempfen
DE3505351A1 (de) 1985-02-15 1986-08-21 Linde Ag, 6200 Wiesbaden Adsorber- oder katalysatoreinheit sowie verfahren zur adsorptiven oder katalytischen behandlung eines fluidstromes
DE3729517A1 (de) 1987-09-03 1989-03-16 Siemens Ag Adsorptionseinrichtung zur gastrennung
DE19754185C1 (de) 1997-12-06 1999-02-04 Deg Engineering Gmbh Reaktor für die katalytische Umsetzung von Reaktionsmedien, insbesondere von gasförmigen Reaktionsmedien
DE19809200A1 (de) 1998-03-04 1999-09-09 Linde Ag Apparat mit durchströmter Schüttung und Verfahren zum Betreiben eines derartigen Apparats
EP1195193B1 (fr) 2000-10-05 2003-11-19 Ballard Power Systems AG Réacteur à plaques pour échange de chaleur
WO2003095924A1 (fr) 2002-05-10 2003-11-20 Chart Heat Exchangers Limited Partnership Echangeurs de chaleur
EP1434652B1 (fr) 2001-10-12 2005-02-16 GTL Microsystems AG Reacteur catalytique
EP1361919B1 (fr) 2001-02-21 2005-05-11 Protensive Limited Reacteur pour realiser des reactions endothermiques
DE10361515A1 (de) 2003-12-23 2005-07-28 Basf Ag Verfahren zur Überwachung, Steuerung und/oder Regelung von Reaktionen eines fluiden Reaktionsgemisches in einem Reaktor mit Thermoblechplatten
WO2006075163A2 (fr) 2005-01-12 2006-07-20 Chart Heat Exchangers Lp Inserts amovibles d'echangeur de chaleur
EP1430265B1 (fr) 2001-09-20 2006-11-15 Catator Ab Dispositif et procede permettant de realiser des reactions catalytiques dans un echangeur a plaques
EP1284813B1 (fr) 2000-05-11 2007-08-01 Methanol Casale S.A. Reacteur utilise pour des reactions heterogenes exothermiques ou endothermiques
DE112006000447T5 (de) 2005-03-05 2008-01-17 Compactgtl Plc, Abingdon Katalytische Reaktoren
EP1975539A2 (fr) 2001-10-29 2008-10-01 CHART HEAT EXCHANGERS Limited Partnership Échangeurs thermiques
US20080282888A1 (en) * 2007-05-18 2008-11-20 Deckman Harry W Temperature swing adsorption of CO2 from flue gas using a parallel channel contractor
US20100224565A1 (en) * 2009-03-06 2010-09-09 Dunne Stephen R Multiple bed temperature controlled adsorption
EP2718086B1 (fr) 2011-06-07 2020-12-02 3M Innovative Properties Company Réglage de position de filière à fente

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1601215B2 (de) 1967-11-03 1971-11-18 Linde Ag, 6200 Wiesbaden Plattenwaermetauscher insbesondere als spaltgaskuehler
GB1572737A (en) 1977-01-17 1980-08-06 Exxon France Heat pump
DE3049889A1 (de) 1979-09-20 1982-03-04 Tech Ind Therm Cetiat Centre Refrigeration process and device
DE3318098A1 (de) 1983-05-18 1984-11-22 Linde Ag, 6200 Wiesbaden Verfahren und reaktor zur durchfuehrung einer endo- oder exothermen reaktion
DE3411675A1 (de) 1984-03-27 1985-10-10 Josef Hubert 5203 Much Schick Vorrichtung zum waerme- und stoffaustausch zwischen zwei oder mehr stroemungsfaehigen medien
FR2590356B1 (fr) 1985-11-19 1989-06-02 Jeumont Schneider Dispositif pour la production en continu de chaud et de froid
DE3710823A1 (de) 1987-04-01 1988-10-13 Bavaria Anlagenbau Gmbh Verfahren zur herstellung geschweisster plattenwaermetauscher, insbesondere kreuzstrom-plattenwaermetauscher
AU581825B1 (en) 1987-08-28 1989-03-02 Union Industry Co., Ltd Adsorption refrigeration system
US5441716A (en) * 1989-03-08 1995-08-15 Rocky Research Method and apparatus for achieving high reaction rates
DE4132015A1 (de) 1991-09-26 1993-04-01 Basf Ag Thermoplastische polyurethan-elastomere mit einem geringen organischen kohlenstoffabgabewert, verfahren zu ihrer herstellung und ihre verwendung
DE19644938A1 (de) 1996-10-29 1998-04-30 Lutz Johannes Adsorptionskältemaschine und Verfahren zu deren Betrieb
DE19944426C2 (de) 1999-09-16 2003-01-09 Balcke Duerr Energietech Gmbh Plattenwärmetauscher und Verdampfer
DE10108380A1 (de) * 2001-02-21 2002-09-05 Deg Intense Technologies & Ser Reaktor zur Durchführung von katalysierten Reaktionen
JP4212888B2 (ja) * 2002-12-26 2009-01-21 三菱化学エンジニアリング株式会社 プレート型触媒反応器
DE102006011409B4 (de) 2005-12-07 2008-02-28 Sortech Ag Adsorptionsmaschine mit Wärmerückgewinnung
DE102006008786B4 (de) * 2006-02-24 2008-01-17 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Adsorptions-Wärmepumpe, Adsorptions-Kältemaschine und darin enthaltene Adsorberelemente auf Basis eines offenporigen wärmeleitenden Festkörpers
DE202006014118U1 (de) 2006-09-14 2006-11-16 Krause, Roman Tunnelzeltmarkise als Sicht- und Wetterschutz
DE102008053828A1 (de) * 2008-10-30 2010-05-12 Airbus Deutschland Gmbh Verbessertes Adsorptionskühlsystem und Adsorptionskühlverfahren für ein Luftfahrzeug
EP3021962A1 (fr) 2013-07-19 2016-05-25 InvenSor GmbH Machine frigorifique à adsorption dotée d'un agent d'adsorption, procédé de production de froid et utilisation d'une zéolite désaluminée en tant qu'agent d'adsorption dans une machine frigorifique à adsorption
BR112016016131B1 (pt) 2014-01-10 2023-03-07 Bry Air [Asia] Pvt. Ltd Dispositivo de troca de calor de adsorvedor híbrido e método de fabricação
JP6200911B2 (ja) * 2015-03-03 2017-09-20 株式会社豊田中央研究所 ヒートポンプ及び冷熱生成方法
DE102015214374A1 (de) 2015-07-29 2017-02-02 Vaillant Gmbh Adsorptionswärmepumpe mit Plattenwärmetauscher

Patent Citations (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1272891B (de) 1960-09-16 1968-07-18 Union Carbide Corp Verfahren zum Reinigen von Gasen oder Daempfen
DE3505351A1 (de) 1985-02-15 1986-08-21 Linde Ag, 6200 Wiesbaden Adsorber- oder katalysatoreinheit sowie verfahren zur adsorptiven oder katalytischen behandlung eines fluidstromes
DE3729517A1 (de) 1987-09-03 1989-03-16 Siemens Ag Adsorptionseinrichtung zur gastrennung
DE19754185C1 (de) 1997-12-06 1999-02-04 Deg Engineering Gmbh Reaktor für die katalytische Umsetzung von Reaktionsmedien, insbesondere von gasförmigen Reaktionsmedien
DE19809200A1 (de) 1998-03-04 1999-09-09 Linde Ag Apparat mit durchströmter Schüttung und Verfahren zum Betreiben eines derartigen Apparats
EP1284813B1 (fr) 2000-05-11 2007-08-01 Methanol Casale S.A. Reacteur utilise pour des reactions heterogenes exothermiques ou endothermiques
EP1195193B1 (fr) 2000-10-05 2003-11-19 Ballard Power Systems AG Réacteur à plaques pour échange de chaleur
EP1361919B1 (fr) 2001-02-21 2005-05-11 Protensive Limited Reacteur pour realiser des reactions endothermiques
EP1430265B1 (fr) 2001-09-20 2006-11-15 Catator Ab Dispositif et procede permettant de realiser des reactions catalytiques dans un echangeur a plaques
EP1434652B1 (fr) 2001-10-12 2005-02-16 GTL Microsystems AG Reacteur catalytique
EP1975539A2 (fr) 2001-10-29 2008-10-01 CHART HEAT EXCHANGERS Limited Partnership Échangeurs thermiques
WO2003095924A1 (fr) 2002-05-10 2003-11-20 Chart Heat Exchangers Limited Partnership Echangeurs de chaleur
DE10361515A1 (de) 2003-12-23 2005-07-28 Basf Ag Verfahren zur Überwachung, Steuerung und/oder Regelung von Reaktionen eines fluiden Reaktionsgemisches in einem Reaktor mit Thermoblechplatten
WO2006075163A2 (fr) 2005-01-12 2006-07-20 Chart Heat Exchangers Lp Inserts amovibles d'echangeur de chaleur
US20080000624A1 (en) * 2005-01-12 2008-01-03 Keith Symonds Removable Heat Exchanger Inserts
DE112006000447T5 (de) 2005-03-05 2008-01-17 Compactgtl Plc, Abingdon Katalytische Reaktoren
US20080282888A1 (en) * 2007-05-18 2008-11-20 Deckman Harry W Temperature swing adsorption of CO2 from flue gas using a parallel channel contractor
US20100224565A1 (en) * 2009-03-06 2010-09-09 Dunne Stephen R Multiple bed temperature controlled adsorption
EP2718086B1 (fr) 2011-06-07 2020-12-02 3M Innovative Properties Company Réglage de position de filière à fente

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
BAKER ET AL.: "The Course of Liquor Flow in Packed Towers", TRANS AICHE, vol. 31, 1935, pages 296 - 315
K. SALEM: "Dissertation", 2006, CUVILLIER-VERLAG GÖTTINGEN, article "Instationäre Temperatur- und Konzentrationsfelder in hochbelasteten Festbettadsorbern"

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114042363A (zh) * 2021-10-28 2022-02-15 西安建筑科技大学 一种抑制脱硫脱硝活性炭自燃的吸附塔及方法
CN114042363B (zh) * 2021-10-28 2024-04-09 西安建筑科技大学 一种抑制脱硫脱硝活性炭自燃的吸附塔及方法

Also Published As

Publication number Publication date
DE102020007212A1 (de) 2021-07-01
WO2021121451A1 (fr) 2021-06-24
WO2021121450A1 (fr) 2021-06-24
WO2021121452A1 (fr) 2021-06-24
DE102020007213A1 (de) 2021-06-17
DE102020007211A1 (de) 2021-06-17
DE102020007214A1 (de) 2021-07-01

Similar Documents

Publication Publication Date Title
WO2021121453A1 (fr) Dispositif et procédé pour traiter un gaz chargé en composants nuisibles et/ou utiles
DE10230342C1 (de) Membranmodul zur Wasserstoffabtrennung
DE2461562B2 (de) Gasadsorbergefäß
EP0376356B1 (fr) Méthode et procédé pour séparer des composants indésirables d'un gaz d'échappement
EP0892225B1 (fr) Appareil de conditionnement d'air et ses composants
DE102017001114B4 (de) Vorrichtung und Verfahren zum Behandeln eines mit Schadstoffen belasteten Gases
WO2010112433A2 (fr) Accumulateur de fluide de travail, échangeur de chaleur et pompe à chaleur
DE60023394T2 (de) Wärmetauscher
WO2009138109A1 (fr) Procédé et dispositif de régénération thermique de matières en vrac chargées par adsorption et/ou absorption
DE4339025C2 (de) Vorrichtung zur Reinigung schadstoffbeladener Abluft
DE102010014643A1 (de) Rohrbündelreaktor
DE2809567C2 (fr)
DD231742A5 (de) Verfahren und vorrichtung zur entfernung unerwuenschter gasfoermiger bestandteile aus einem rauchgas
DE60317126T3 (de) Verfahren und Vorrichtung zur Entfernung von Distickstoffmonoxid
DE2548290A1 (de) Verfahren und vorrichtung zum zerlegen von luft
DE4135018A1 (de) Verfahren und vorrichtung zur stroemungsfuehrung in radialstromreaktoren
WO2012069156A2 (fr) Dispositif de filtration et procédé de nettoyage d'un courant de gaz
EP1621250B1 (fr) Réacteur pour réalisation de réactions fortement exothermiques avec augmentation de pression
DE2204702A1 (de) Vorrichtung zur Behandlung von Gasen, welche zusätzlich zu Feststoffen unerwünschte Verbindungen enthalten
WO1996004065A1 (fr) Reacteur a adsorption utilise pour extraire les composants indesirables d'un fluide
DE2601181C2 (de) Vorrichtung zur thermischen Reinigungsbehandlung eines Abgases
DE3702845A1 (de) Vorrichtung und verfahren zum trocknen von gasen
EP0191441A1 (fr) Procédé pour éliminer des composants indésirables d'un gaz de fumée
DE10030753A1 (de) Verfahren und Vorrichtung zur Desorption von Adsorbern
EP0123242A2 (fr) Echangeur de chaleur, chauffé par le gaz des fumées, pour fournaux à combustible sulfureux

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20842172

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 20842172

Country of ref document: EP

Kind code of ref document: A1